Process for treating hydrocarbons



Feb. 23, 1932. w. RI HOWARD Re. 18,357

PROCESS FOR TREATING HYDROCAHBONS Original Filed Sept. 8, 1919 A T TORNE Y.

neck 13.

Reisaued Feb. 23, 1932 UNITED STATES WILLIAM R. HOWARD, OF WASHINGTON,DISTRICT 013' COLUMBIA, ASSIGNOB TO UNIVERSAL OIL PRODUCTS COMPANY, OICHICAGO, ILLINOIS, A CORPORATION OF SOUTH DAKOTA PROCFfiS FOR TREATINGHYDBOGABBONB Original No. 1,535,725, dated April 28, 1925. Serial No.322,457, died September 8, 1918. Application for reissue filed March 10,1927. Serial No. 174,342.

This invention relates primarily to the socalled cracking of petroleumoil or in other words, to the conversion of high boiling point to lowboiling point hydrocarbons such as gasoline. The process is preferablyoperated as a continuous one in which the oil passes through a crackingzone to a vapor chamber, thence the vapors are subjected to a refluxcondensing action and finally to a water condenser.

In the present invention, the refluxed condensate instead of returningto the original cracking zone is delivered to a separate chamber andrevaporized. This prevents the lighter vapors from being over-treatedand also prevents carbon from being returned to the primary crackingzone.

As a further feature of the invention, it may be so carried out as tosubject the reflux condensate to a different pressure and temperaturethan that to which the oil is first subjected.

Referring in detail to the drawing, 1 desi nates a fire box in which ismounted an en less'heating coil 2, which forms a cracking zone. Oil issupplied to this coil 2 through pipe 3 from pump 4 from any suitablesource of supply. The oil passes into vapor or expansion chamber 5through pipe 6. The vapars generated pam out through vapor line into thestandard 8 of an aerial condenser 9. It is to be noted that the pipe 7enters the standard 8 at a point above the lower end of the latter andis provided with a check valve 10. The arrangement is such that thevapors can pass through the pipe 7 only in the direction of the arrow.The unvaporized oil is drawn out through the drawofi pipe 11, controlledby valve 12. The heavier va- Ears in the aerial 9 will condense and fallack into the standard 8. The uncondensed vapors pass out through thegooseneck 13 into coil 14 in water condenser 15. From coil 14 thecondensed vapors and incondensable gases means of pipe 17. A gas outlet18 controlled by valve 19 is provided, as is also a liquid drawoif pipe20 controlled by valve 21. A

valve-22 may also be provided in the goosemay the still 24 and return.pass into receiving tank 16 by.-

The condensed distillates which fall back into the standard 8 passthrough line 23 into the secondary still 24. This still 24 is seated ina furnace 25 so that it can be heated. The vapors generated in the still24 pass out through line 26 into the standard 8 and are subjected to thecondensin action of the aerial reflux condensers. heck valves 27 and 28.are interposed in the lines 23 and 26 and so arranged that the oil andva ors can pass through the lines 23 and 26 on y in direction of thearrows. A drawoif line 29 leads from the lower end of the still 24 andis provided with valve 30.

As a feature of the invention a pump P is interposed in the line 23 andso arranged as to be able to force the condensed liquid coming from thestandard 8 into the secondary still 24. A pressure valve R is interposedin the return line 26.

The oil to be treated may be of any desired character and the pressureand temperature used may be varied within relatively wide limits. Thefollowing illustrative run on gas oil from the Kansas may be given. Thewhole system maybe kept under a pressure of say 100 lbs. by controllingthe various outlet valves, or if desired, the pressure of 100 lbs. maybe maintained onthe still 2 and a pressure of 150 lbs. or moremaintained on the contents of the still 24. Moreover, the pressure inthe still 24 may be raised or lowered by regulating the valve R as theprocess proceeds; as for example, raised to 200 ounds or lowered to 125pounds.

T e oil temperature in the coil 2 ma be 650 F. while the temperature inthe sti l 24 be 800 F. The reason for this is that the charging stockcontains more low boiling point constituents than does the condensatereturning to the still 24. It will be seen that the partially crackedrefluxed condensate is in eflect shuttle cocked, from the aerial to Itwill also be noted that any carbon precipitated in the reflux condensatewill go back to the tank and not reach the coil 2. By properlyregulating the size of the aerial 9 substantial] any en point gasolinemay be made. In 0 er words with a given gas oil the aerial 9 can-be ofsuch size that it will be at all times kept at a temperature of 400 F.,hence nothing boiling above 400 F. will pass out through the gooseneck13. It is to be understood that a regulated quantity of oil isconstantly fed to the apparatus. The pipes 23 and 26 are provided withvalves 31 and 32 whereby the still 24 can be cut out of the system forcleaning if desired.

I claim as my invention 1. A process of converting relatively heavyhydrocarbons into those of lower boiling point, consisting in passingthe oil continuously through a crac ing zone, thence to a vapor chamberpassing the vapors from said vapor chamber to a reflux condenser,passing the uncondensed portion of the vapors from the reflux condenserto a final condenser and receiving tank, returning the liquid portioncondensed in the reflux condenser under forced pressure to a secondarycracking zone, distilling the liquid portion in said zone and againpassing the vapors generated to the reflux condenser, continuouslyretreatin the reflux condensate in said secondary cracking zonemaintaining a predetermined superatmospheric vapor pressure on the oilin said first cracking zone, an maintaining a higher vapor pressure onthe oil in said secondary cracking zone.

2. A process of converting relatively heavy hydrocarbons into those oflower boiling point, consisting in passing the oil through a crackingzone, thence to a vaporizing zone, passing the vapors from the vaporzone and subjecting them to a refluxing action, passing the uncondensedportion of the vapors to a final condenser and receiving tank and thecondensed portion to a secondary cracking zone, causing vapors generatedin said latter zone to again pass to the refluxing zone, maintaining apredetermined superatmospheric vapor pressure on the oil in said firstcracking zone and maintaining a higher vapor pressure on the oil in saidsec- Ol'lClflIZ cracking zone.

3. process of converting relatively heavy hydrocarbons into the lowerboiling point hydrocarbons, consisting in passing 01 through a crackingcoil and thence to a reacting zone, in discharging vapors from thereacting zone to a dephlegmator, in discharging uncondensed vapors fromthe dephlegmator for condensation and collection, in passing refluxcondensate from said dephelgmator to a second still for treatment, inmaintaining an increased pressure and temperature in said second still,and in introducing the vapors from said second still to saiddephlegmator.

4. A process of converting relatively heavy hydrocarbons into the lowerboiling point hydrocarbons, consisting in passing oil through a crackingcoil and thence to a reacting zone, in discharging vapors from thereacting zone to a dephlegmator, in discharging uncondensed vapors fromthe dephlegmator for condensation and collection, in passing refluxcondensate from said dephlegmator to a second still for treatment, inmaintaining an increased pressure and temperature in said second still,in introducin tl vapors from said second still to said deplilegmator,and in maintaining a superatmospheric pressure on the oil undergoingdistillation in each still.

5. An oil conversion process consisting in subjecting charging oil tocracking conditions of temperature and pressure suflicient to convert asubstantial ortion of said oil into gasoline-like materials withoutsubstantially overheating the lighter fractions of the gasoline thusproduced, in removing unvaporized residue from said cracking operation,in separating the vapors generated into a light gasoline-like materialand a heavier refractory condensate, in continuously subjecting saidrefractory condensate to a substantially increased temperature andpressure while maintained in an independent heating zone whollysegregated from the unvaporized fractions of said charging oil and inwhich zone a pool of such condensate undergoes cracking.

6. An oil converting process consisting in subjecting charging oil tocracking conditions of temperature and pressure suflicient to convert asubstantial quantity of said oil without overcracking the light gasolinefractions produced therefrom, in removing the unvaporized residue ofsuch crackingi operation in separating the light so cientlfy crackedgasoline-like vapors from the insu ficiently cracked vapors to form fromthe latter a refractory condensate, in subjecting said con ensate to atemperature and pressure exceeding the temperature and pressuremaintained on the charging 011 and sufficient to convert said refractorymaterial into light gasoline-like constituents while a substantialportion of such condensate is in a liquid condition and while thecondensate is maintained isolated from the unvaporized charging oil, andin collecting the ight gasolinelike constituents produced from both thecharging oil and the reflux condensate to form a gasoline-(likematerial.

7. An oil converting process consisting in subjecting charging oil to acracking temperature while under a pressure of at least 100 pounds persquare inch to convert a substantial portion of said oil, in removingthe unvaporlzed, residue of such conversion, in subjecting the vaporsgenerated to reflux condensation to separate the heavy from the lightervapors, and in subjecting a body of the reflux condensate to atemperature substantially above the temperature to which the chargingoil is subjected and to a pressure of not less than 125 pounds persquare inch while said condensate is wholly se regated from theunvaporized residue, an in collecting the products of such conversion.

8. A method .of making gasoline which consists in subjecting chargingoil to crack ing conditions of temperature and pressure to convert theoil to produce hydrocarbon substances containing gasoline and heavierfractions, in separating the heavier fractions from the lightergasoline-like products thereby producing a refractory distillate, and insub ecting such distillate to a substantially increased temperature andpressure in an independent cracking zone where the distillate issegregated from the unvaporized fractions of the charging oil and inwhich zone a liquid body of said distillate undergoes cracking.

9. An oil conversion process consisting in subjecting charging oil tocracking conditions of temperature and pressure suflicient to convert asubstantial portion of said oil into gasoline-like materials, inseparating the products of conversion into a light gasolinelike materialand a heavier refractory distillate, lll continuously subjecting saidrefractory distillate to a substantially increased condition oftemperature and pressure while the distillate is maintained whollysegregated from the unvaporized fractions of the chargin oil and asubstantial portion thereof is In liquid condition while it isundergoing cracking and in recovering the gasoline-like products of suchconversion.

10. An oil conversion process consisting in subjecting charging oil to acracking temperature while under a pressure of at least 100 pounds persquare inch to convert a substantial quantity of such oil into 11 hterproducts, in separating such lighter pro nets into gasoline-likefractions and a heavier refractory il, and in subjecting a body of saidheavier refractory oil to a temperature above the temperature to whichthe charging oil is subjected and a pressure of not less than 125 poundsper square inch while such refractory material is se regated from theunvaporized residue of t e charging oil and in collecting the productsof conversion.

11. A method of making gasoline which consists in subjecting chargingoil to cracking conditions of temperature and a superatmosphericpressure to convert the oil to produce hydrocarbon substances containinggasoline and heavier fractions, in separating the heavier fractions'fromthe lighter gasoline-like products thereby roducing a refraetorvdistillate, and in su jecting a liquid body of such distillate to acracking temperature while under a substantially increased pressure inan independent cracking zone where the distillate remains segregate fromthe unvaporized fractions of the charging oil.

12. An oil conversion process consisting in subjecting charging oil tocracking conditions of tem erature and super-atmospheric pressuresuflibient to convert a substantial portion of said oil intogasoline-like materials, in separating the roducts'of conversion into alight gasoline-1i e material and a heavier refractory distillate, incontinuously subjecting said refractory distillate to a crackingtemperature while a substantial portion thereof is maintained in aliquid condition b a superatmospheric pressure substantially exceedingthe pressure maintained on the charging oil, and in maintaining suchdistillate segregated from the unvaporized fractions of the charging oilduring the conversion thereof, and in recovering the products ofconversion.

13. An oil conversion process consisting in subjecting charging stock toa cracking temperature while under a pressure of at least one hundredpounds per square inch to convert a substantial quantity of such oilinto lighter products, in separating the products of conversion into alight gas0line-like material and a heavier refractory distillate, and insubjecting a body of said distillate in a liquid condition to a crackingtemperature While under a pressure of not less than a hundred andtwenty-five pounds per square inch and while such distillate issegregated from the unvaporized residue of the charging stock.

14. A process for cracking hydrocarbon oil comprising continuouslyadvancing a. stream of charging oil through a heating zone where it issubjected to a cracking temperature and thence delivered to an enlargedzone, main taining a superatmospherie pressure on said oil stream and inthe enlarged zone, in continuously removing vapors generated from theoil from thevenlarged zone while withdrawing unvaporized oil from suchenlarged zone to maintain the vapors produced of a substantially uniformcomposition throughout the normal run of the process, in condensingheavier vapors Without condensing the lighter asoline-like vapors,thereby producing a re ractory distillate of substantially uniformcomposition, and in continuously subjecting such distillate to acracking tempera-ture substantially greater than the temperature towhich the charging oil is initially heated While maintained in anindependent cracking zone segregated from the initial charging oilundergoing conversion to convert substantial portions of said distillateinto gasoline-like products.

15. A process for cracking hydrocarbon oils comprising continuouslysupplying charging oil to an initial cracking zone to be subjected to acracking temperature while maintained under a superatmospheric pressureto volatilize substantial portion thereof forming gasoline-likematerials and products heavier than gasoline in maintaining the productsof conversion of a substantially uniform composition b removing from theinitial cracking zone t e unvaporized fraction of the charging oil, inseparating the converted volatile products into light gasolinelikematerial and a heavier refractory distillate, and in continuouslysubjecting said refractory distillate, of a substantially uniform comosition, to a cracking temperature excecding the temperature to whichthe charging oil is initially heated while maintained segregated fromthe charging oil in the initial crackin zone whereb substantial portionsof said refractory istillate are converted into additional gasoline-likeproducts.

16. A rocess for cracking hydrocarbon oil comprising continuouslysupplying charging oil to be converted to an initial cracking zone whereit is subjected to a cracking temperature while maintained under asuperatmospheric pressure, in continuously removing from said crackingzone constituents volatilizing at the temperature and pressuremaintained therein, in removin from said initial cracking zoneunvaporize fractions of the charging oil -to maintain the volatileproducts produced therein of substantially uniform composition duringthe normal operation of the process, in continuously subjecting thevolatilized products to artial condensation to separate line-li eproducts from the less volatile constituents, in continuously subjectingthe less volatile constituents thus obtained to an independent crackingtemperature substantially "exceeding the temperature maintained in theinitial cracking zone while retaining such distillate segregated fromthe chargin oil undergoing conversion in the initial crac ing zone toconvert additional quantities of said distillate into gasoline-likeproducts.

17. A process for cracking hydrocarbon oil comprising initiallysubjecting charging oil to a cracking reaction by continuously advancinga stream of charging oil through a heating coil to be heated therein toa cracking temperature, in transferring such oil to an enlarged chamber,in maintaining a superatmospheric pressure on the oil undergoigidgtreatment, in separating the volatilized pr nets of conversion into alight gasoline-like material and a heavier refractory distillate, thecomposition of which is substantially uniform during the operation ofthe process in continuously subjecting such refractory distillate ofsubstantially uniform com osition to a temperature substantially exceeing the temperature to which the charging stock is initially heatedwhile maintaining said refractory distillate during its conversion undersuch increased temperature segregated from the charging oil undergoingits initial cracking, and 111 recovering the products of suchconversion.

18. A process comprising continuously supplying charging ior crackinghydrocarbon oil oil to be converted to an initial cracking zone where itis subjected to a cracking temperature while maintained undersuperatmosheric pressure, in continuously removing mm the heated oilvolatilized constituents leaving the oil at the temperature and pressureemployed in the initial cracking zone,

in removing from the cracking zone unvaporized products to maintain thevolatilized products produced therein of substantially uniformcomposition, in separating such volatilized products into alightgasoline-like material and a heavier refractory distillate, the comosition of which remains substantially uni orm during the operation ofthe process, and in continuously subjecting such distillate to acracking temperature while under a substantially increased pressure inan independent cracking zone where the distillate remains segregatedfrom the charging oil undergoing conversion in the initial crackingzone.

WILLIAM R. HOWARD.

DISCLAIMER Re. No. l8,857.-William R. Howard, Washington, D. C. PROCESSFOR TREATING HYDBOCARBONS. Patent dated February 23, 1932. Disclaimerfiled July 22, 1938, by the patenbee the assignee, Universal OilProducts Company, approving and concurring.

Hereby enters this disclaimer to the subject matter constituting claims11, 12, and 13 of said reissue patent.

[Ofliaial Gazette August 16', 1988.]

